To date there has been much work carried out in the field of surface science to gain a better understanding of the fundamentals of a wide range of catalytic systems and reactions. The central theme of this thesis relates to cobalt based Fischer-Tropsch synthesis (FTS) with particular focus on the structure, composition and surface chemistry of CoPd bimetallic systems and on the interaction of Co with oxide support materials. In the work described in this thesis MEIS and STM are used to examine the growth of Co on Pd{111} and to characterise the structure of CoPd alloys created by thermal treatment of thin Co films. MEIS investigations indicate that Co grows initially as an fcc overlayer, but beyond a few layers, a stacking fault exists resulting in hcp growth. On annealing between 550 and 700 K, a previously unreported ordered surface alloy is observed giving rise to a p(2 x 1) structure which is concluded to be the surface termination of an ordered CoPd bulk alloy. At higher annealing temperatures, long range Moiré structure is observed by STM which MEIS reveals to correspond to a Pd-rich alloy. MEIS is used to investigate adsorbate induced segregation effects at CoPd surfaces on Pd{111}. The adsorption of O2, CO, H2 and CO/H2 mixtures (syngas) were all examined on a range of bimetallic surfaces. Oxygen adsorption on CoPd alloys strongly segregates cobalt to the surface as a result of the facile oxidation reaction. The behaviour of the components of syngas was more complex with the most noticeable effects being observed on surfaces which were more defect rich. The growth, annealing behaviour and adsorption properties of Co particles on oxide and mixed oxide surfaces are examined using MEIS and TPD.

The entrainment rate of Ferrosilicone (FeSi) particles was measured in a 140 mm perspex column with air as the fluidising medium. Two different types of FeSi were used, namely atomised FeSi, which is mostly spherical in shape with smooth surfaces, and milled FeSi, which is irregular with rough surfaces. Both the FeSi mixtures had the same solid density and the similar average particle diameters ranging from 38 µm to 50 µm. The size and density of these particles put them on the border between Geldart A and Geldart B powders, similar to the high temperature Fischer-Tropsch catalyst. The atomised FeSi had a slightly higher concentration in fines (8.6% vs 1.8%), but except for the difference in particle shape, the two mixtures had otherwise very similar physical properties. A substantial difference in entrainment rate was measured between the atomised and milled FeSi, where the atomised had an entrainment rate of about six times higher than the milled FeSi throughout the range of superficial velocities tested. It was shown that the higher entrainment rate cannot be attributed only to the higher fines concentration, but that the difference in particle shape had a significant effect on the entrainment rate. Several two dimensional shape characterisation techniques were used in attempt to quantify the difference between the atomised and the milled FeSi. Of these the particle circularity managed to differentiate the best between the two particle mixtures. The circularities of the atomised and the milled FeSi were found to be 0.782 and 0.711 respectively. The measured circularity was used instead of a sphericity to adjust for the effect of particle shape on the terminal velocity of the particles. The adjusted terminal velocity was then used in the elutriation rate constant correlations to see which of the popular correlations in literature predicts the entrainment rate of the FeSi the best. All of the correlations gave a poor performance in predicting the measured entrainment rates. The two correlations that performed the best were that of Choi et al. (1999) (AARE = 72.6%) and Geldart et al. (1979) (AARE = 79%). It was concluded that single particle drag and single particle terminal velocities are not adequate to incorporate the effect of particle shape on entrainment rate. The method i by which shape affects entrainment rate therefore deserves further investigation. Further studies should also be done to develop a three dimensional shape descriptor that predicts bulk behaviour better. / Dissertation (MEng)--University of Pretoria, 2008. / Chemical Engineering / unrestricted

Energy carriers, such as coal, natural gas and biomass, can be converted by Fischer-Tropsch technology into synthetic crude (syncrude). Fischer-Tropsch derived syncrude can then be refined to transportation fuels, such as motor-gasoline, jet fuel and diesel fuel. These fuels meet the same specifications as crude oil derived transportation fuels. Conventional refining technologies have to be adapted to deal with Fischer-Tropsch syncrudes, because they differ significantly from crude oil with respect to composition. Some of the key differences are the high concentration of oxygenates and olefins and absence of sulphur in Fischer-Tropsch syncrude. Imposing a crude oil refining methodology on syncrude can lead to unwieldy and expensive refineries. Yet, despite an abundance of literature of Fischer-Tropsch synthesis, there is little literature that deals with the refining of Fischer-Tropsch syncrude. The present study investigated current refining practice for both crude oil and Fischer-Tropsch syncrude in order to identify fundamental differences in their refining focus and conversion behaviour. This was followed by a critical evaluation of the compatibility of syncrudes from high temperature Fischer-Tropsch (HTFT) and low temperature Fischer-Tropsch (LTFT) synthesis with the chemistry and catalysis of various conversion processes. The conversion processes that were evaluated include isomerisation, oligomerisation, etherification, alkylation, metathesis, hydrogenation, hydroisomerisation, hydrocracking, catalytic cracking, coking, thermal cracking, catalytic reforming and dehydration. The recommendations from the technology evaluation provided the foundation for the development of Fischer-Tropsch syncrude based refinery designs. Refinery designs were developed to determine configurations that would maximise the production of on-specification motor-gasoline, jet fuel and diesel fuel respectively. It could be shown that less complex refinery designs were required to refine Fischer-Tropsch syncrude to motor-gasoline and jet fuel, than were required for crude oil refining. It was also shown that on a molecular level Fischer-Tropsch syncrude is unsuited for maximising the production of Euro-4 type diesel fuel. The present study illustrates the advantage of considering fundamentals in developing refineries specifically for Fischer-Tropsch syncrude, rather than imposing crude oil design practises on Fischer-Tropsch syncrude refinery designs. / Thesis (PhD (Chemical Engineering))--University of Pretoria, 2008. / Chemical Engineering / unrestricted

Etwa ein Drittel des Gesamtendenergieverbrauchs entfällt auf den Transportsektor, dessen Energieverbrauch zu rund 98 % über fossile Kraftstoffe (maßgeblich Mineralöl) abgedeckt wird [70], [71], [91]. Gleichzeitig ist der Transportsektor eine der Hauptursachen für den Ausstoß anthropogener Treibhausgasemissionen. Mobilität (insbesondere von Personen und Gütern) ist für die gesellschaftliche und wirtschaftliche Entwicklung unverzichtbar und nach wie vor ein überdurchschnittlich wachsender Bereich [103]. Weltweit wird sich die Anzahl der Kraftfahrzeuge von ca. 700 Mio. Personenwagen im Jahr 2000 auf etwa 1,3 Mrd. Personenwagen im Jahr 2030 nahezu verdoppeln; gleiches gilt für den damit einhergehenden Verbrauch an Endenergie [302]. Hingegen wird in Deutschland von einem um 9 % sinkenden Energieverbrauch gegenüber 2005 auf 2 EJ/a im Jahr 2030 ausgegangen; in den Mitgliedsstaaten der EU-27 hingegen wird ein Anstieg um 14 % gegenüber 2005 auf 17,7 EJ/a im Jahr 2030 erwartet [71], [72]. [... aus der Einleitung]

This thesis deals with the study of several catalysts for the Fischer-Tropsch synthesis in the Biomass-To-Liquid process. In this work two groups of catalysts were tested. On the one hand, two series of catalysts with cobalt loadings of 6 and 12 wt% over SiO2 and some of them containing 5wt% of TiO2 were tested. One the other hand, other two series of mesoporous short channel SBA-15, all of them with cobalt loadings of 12wt% and some with 5wt% of titania. The first series was supported on SBA-15 DeWitte and the second one on SBA-15 Martinez. On the one hand, the influence of water addition to the feed, titania content and cobalt loading to the catalyst and was studied, as well as the consequences of a GHSV. The FT reaction was carried out along 5 periods of 24 hours each, in which conditions such as feed and water content were modified, enabling the study of these parameters. It was found that water provokes an increase of the CO conversion and has a positive kinetic effect on the rate to hydrocarbons. However, this fact reaction is followed by a quick deactivation, enhanced by high water partial pressures. Most of that deactivation is irreversible since it is not completely recovered after water removal. On the other hand, differences between the supports were studied. Some SBA-15 supported catalysts show CO diffusion limitations at longer channel lengths than what applies for conventional 3D porous supports. Titania grafting increases the rate to hydrocarbons, showing positive results for FT catalysts development.

[pt] Catalisadores de ferro suportados em sílica alumina e em sílica mesoporosa, além de nano partículas de ferro não suportadas, foram estudados. A preparação dos catalisadores suportados ocorreu pelo método de impregnação do ponto úmido incipiente com soluções aquosas de cloreto de ferro, para obter 2 por cento ou 5 por cento de metal, sendo um desses preparado pelo método da ureia, onde uma quantidade apropriada de uma solução aquosa de FeCl3·6H2O (99 por cento -Merck) foi misturada com ureia. As amostras foram caracterizadas por medidas de fisissorção de N2, difração de Raios-X (DRX), redução com temperatura programada (RTP) e microscopia eletrônica de transmissão (TEM). A quantidade de metal foi determinada usando espectroscopia de absorção atômica (EAA). Os suportes de sílica alumina e de sílica mesoporosa foram caracterizados ainda por análise termogravimétrica (ATG/DTG). As propriedades texturais mostraram que após a introdução do metal nos suportes, a área específica, o volume de poros e o diâmetro de poro decresceram conforme o teor metálico foi aumentado. As análises de DRX com refinamento de Rietveld detectaram a formação das fases de FeO, Fe3O4, Fe0, para todas as amostras suportadas. Os perfis de redução (RTP) para as amostras de ferro suportadas mostraram, principalmente, duas regiões de redução, a primeira atribuída a redução de Fe2O3 para FeO e a segunda a redução de FeO para Fe0. / [en] Iron catalysts supported on silica alumina and mesoporous material, beside non supported iron nanoparticles, were studied. The preparation of supported catalysts occurred by incipient wetness impregnation method with aqueous solutions of iron chloride to give 2 percent or 5 percent of metal. One iron catalyst supported on silica alumina was prepared by the method of urea, in which an appropriate amount of an aqueous solution of FeCl3·6H2O (99 percent - Merck) was mixed with urea for impregnation. The samples were characterized by measurements of N2 physisorption, X-ray diffraction (XRD), temperature programmed reduction with (TPR), transmission electron microscopy (TEM). The amount of metal embedded in each sample was determined using atomic absorption spectroscopy (AAS). The silica alumina and mesoporous silica supports were also characterized by thermogravimetric analysis (DTA/TGA). The textural properties showed that after introduction of the metal into the supports, the specific area, pore volume and pore diameter decreased as the metal content was increased. XRD analysis with Rietveld refinement showed the formation of phases the following phases FeO, Fe3O4, Fe0, for all supported samples. Reduction profiles (TPR) for the supported iron samples showed mainly two reduction regions, assigned for Fe2O3 to FeO and for FeO to Fe0, respectively.

The following chapters deal with the chemistry, catalytic poisoning, newer catalyst technologies, and possible future solutions to increase the efficiency of creating high-value products by thermochemically converting gasified biomass (producer gas). Chapter 1 puts emphasis on multifunctional catalysts containing transition metals that are used for renewable fuel production. High-value products such as gasoline-range hydrocarbons, dimethyl ether (DME), aldehydes, isobutane, isobutene and other olefins can be produced with gasified biomass due to the gas containing syngas (H2 + CO). The chemistry and production of these chemicals is discussed in the review. Chapter 2 describes the reactor design of a bench scale system and results after using a Mo/HZSM- 5 catalyst for aromatic hydrocarbon creation. This chapter also discusses issues that came with trying to control the temperature without any reactor intercooling. Chapter 3 shows the feasibility of using a particular multifunctional catalyst with a lab scale system and also shows the importance of certain process variables including temperature, space velocity, gas ratios, and pressure. The subject of the importance of the cleanliness of the producer gas is also discussed so that maximum high-value product yield can be achieved with the greatest efficiency. Chapter 4 discusses the implementation of a bench scale and pilot scale reactor design (both with intercooling) and the results of scale-up when using the catalyst mentioned in Chapter 3. Chapter 5 involves the modelling of an industrialized system with Aspen Plus. The economics of industrial plants to produce hydrocarbons from coal or wood feedstocks at scales of 5, 50 and 5000 tons per day were modeled using CAPCOST.

The conversion of biomass to biouel has received considerable attention as a sustainable way to produce energy. As worldwide fossil fuels become depleted these efforts grow in importance. The overall strategy is to transform the parent biomass feedstock to increase C-C bonds while reducing oxygen in the final products. A catalytic approach is often used to achieve good yields of transportation grade liquid hydrocarbons from biomass. Development of novel catalyst systems to aid in the thermochemical conversion of biomass to biouel is the focus of this thesis. Gasification of biomass produces synthesis gas (CO and H2). Synthesis gas can be converted to liquid hydrocarbons using Fischer-Tropsch (FT) synthesis. Mo/ZSM-5 FT catalysts with a potassium (K) promoter are introduced to enhance liquid hydrocarbon production and CO conversion of synthesis gas. Liquid products and CO conversion were determined using GC-MS analysis with respect to changes in K loading from 0-2%. The highest liquid product selectivity (21.7%) was found with 1.0% K loading while largest CO conversion (63%) was found with 1.2% K loading. This catalyst work was extended by introducing Ni and Co into the Mo/ZSM-5 catalysts. A copper based water gas shift catalyst (WGS) was also used in concert with the FT catalyst to improve product selectivity. This WGS catalyst promotes the in-situ production of H2 while decreasing water content. The FT+WGS catalyst were used to convert both 1:1 CO: H2 syngas and bio-syngas at 280 °C and 350 °C. The liquid hydrocarbon selectivity was significantly changed and the CO conversion was remarkably increased compared to the reactions without the dual catalyst at both temperatures. In the fourth chapter, FT+WGS catalysts were studied for upgrading bio-oil model compounds. Guaiacol and furfural were used as the model compounds and upgrading reactions were done under H2, syngas and bio-syngas at 200, 250 and 300 °C. Significant conversion of both guaiacol (85%) and furfural (100%) occurred with syngas at 300 °C. Products upgraded from syngas had a higher combined heat of combustion than the products with pure H2. This suggests the incorporation of some C from CO with model compound upgrading reactions with syngas.

Stable dinuclear complexes bis(heptane-2,4,6-trionato)dicopper(II) [Cu2(daa)2], bis(1,5-diphenyl-1,3,5-pentanetrionato)dicopper(II) [Cu2(dba)2], bis(1,5-diphenyl-1,3,5-pentanetrionato)dicobalt(II) [Co2(dba)2], and [6,11-dimethyl-7,10-diazahexadeca-5,11-diene-2,4,13,15-tetranato(4-)-N7N10O4O13;O2O4O13O15] copper(II)cobalt(II) [(CuCo(daaen)] were supported on Cab-O-Sil by the batch impregnation technique. The supported samples were characterized by UV-Vis, elemental analysis, X-ray powder diffraction (XRD), diffuse reflectance infrared Fourier transform spectroscopy (DRIFTS), and thermal gravimetric analysis (TGA). Elemental analysis and TGA data confirm that the Cu2(daa)2 complex loses one of its coordinated ligands upon adsorption onto silica in THF at greater than 4.43 wt% Cu loading. By contrast, at all Cu loadings the Cu2(dba)2 complex was adsorbed on the silica surface in CH2Cl2 without loss of ligand. XRD and DRIFTS results confirmed the formation of Cu2(dba)2 multilayer films on the Cab-O-Sil surface for samples containing greater than 2.64 wt% copper. The dinuclear cobalt complex and copper-cobalt complex also do not lose their coordination ligands upon adsorption on the surface. These two metal complexes are amorphous and did not produce XRD patterns. However, DRIFTS results confirm that the binuclear cobalt complex and the copper-cobalt complex begin forming multilayer films between 1.21and 2.53 wt% Cu. The Cu2(dba)2/silica precatalysts were subsequently converted to the catalysts by decomposing the organic ligands at 450 degrees Celsius followed by activation with 2% H2 at 250 degrees Celsius and were evaluated for methanol synthesis and methanol decomposition reactions. Kinetic studies demonstrated that the 3.70% Cu/silica[Cu2(dba)2] catalyst is more active for methanol decomposition than it is for methanol synthesis. The supported dinuclear cobalt and copper-cobalt precatalysts were converted to the catalyst by heating at 450 degrees Celsius followed by activation of the catalysts with 50% H2. Four different catalysts, 3.5% Co/silica[Co2(dba)2], 6.7% Co/silica[Co2(dba)2], 2.3% Co/silica[CuCo(daaen)], and 5.5% Co/silica[Co2(daa)2] were evaluated for the Fischer-Tropsch reaction at 350 degrees Celsius in a batch reactor. The supported binuclear cobalt catalyst produced C1-C7 alkanes and a significant amount of CO2. By contrast, the catalyst formed from heterobinuclear CuCo(daaen) showed the ability to convert syngas to aromatics with a narrow product distribution. In addition, the 6.7% Co/silica[Co2(dba)2] multilayer catalysts have above 98% conversion rates and 60% liquid hydrocarbon selectivity in a flow reactor.

No description available.